CN106890662A - A kind of catalyst, its preparation method and its application - Google Patents
A kind of catalyst, its preparation method and its application Download PDFInfo
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- CN106890662A CN106890662A CN201710101812.9A CN201710101812A CN106890662A CN 106890662 A CN106890662 A CN 106890662A CN 201710101812 A CN201710101812 A CN 201710101812A CN 106890662 A CN106890662 A CN 106890662A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/24—Nitrogen compounds
- B01J27/25—Nitrates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/06—Halogens; Compounds thereof
- B01J27/138—Halogens; Compounds thereof with alkaline earth metals, magnesium, beryllium, zinc, cadmium or mercury
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
Abstract
The invention discloses a kind of catalyst, its preparation method and its application, the catalyst is with porous metals fluoride or oxyfluoride as carrier, with precious metal palladium or platinum as main active component, addition Partial Elements are used as co-catalyst, prepared using infusion process, made catalyst is used for gas phase reaction after filtering, dry, roasting, activation.The features such as catalyst prepares active high, selectivity during trifluoro-ethylene reacts high, catalyst long service life for gas phase.
Description
Technical field
The present invention relates to a kind of catalyst, it is more particularly to a kind of for gas phase reaction prepare trifluoro-ethylene catalyst, its
Preparation method and applications.
Background technology
Trifluoro-ethylene is a kind of widely used fluorine-containing organic intermediate, is that synthesis hydrofluoroether, fluorine bromine be oily and fluorine-containing height
The important source material of Molecularly Imprinted Polymer, has application in fields such as electronic apparatus, aviation, cleaning, the energy.
The process route of the production trifluoro-ethylene of current comparative maturity mainly has two kinds：One is with HFC-134a as initial former
Material, trifluoro-ethylene is generated by dehydrofluorination cracking reaction, and the process route is simple, and raw material is easy to get, but process conditions are more severe
Carve, HF is produced in course of reaction, it is higher to equipment requirement, and also HFC-134a conversion ratios are relatively low, and trifluoro-ethylene yield is low, catalysis
The agent life-span is shorter.Patent FR 2710054A1, US 5856593A are reported with Ni/AlF respectively3With chromium base oxide as urging
Agent, the technique that production trifluoro-ethylene is cracked by HFC-134a, feed stock conversion is 30% or so, but due to high temperature carbon distribution,
Catalyst life is very short.
Another route is, with CFC-113 as initiation material, CTFE co-production to be produced by catalytic hydrogenation and dechlorination
Trifluoro-ethylene, patent US 5283379, CN 1460547A, CN 1460549A, CN 1351903A are reported used by the technique
Catalyst, partial catalyst effect has reached the leading level in the world, but this route is main to produce based on CTFE, trifluoro
Content is relatively low wherein for ethene, and the shorter problem of catalyst life is still present.Also have and enter this process route in two steps
OK, CTFE is produced first with CFC-113 hydrogenation-dechlorinations, then to the further hydrogenation-dechlorination production trifluoro second of CTFE
Alkene.This mode is with CFC-113, compared with raw material production trifluoro-ethylene route, the yield of trifluoro-ethylene is carried by a relatively large margin
Rise, patent CN 102211028B report a kind of catalyst that trifluoro-ethylene is produced for CTFE hydrogenation-dechlorination, and this is urged
Agent contains the active component of three kinds and the above, and absorbent charcoal carrier used it is acidified-fluorination treatment, in CTFE plus
Show excellent catalytic performance in hydrogen dechlorination reaction, feed stock conversion and target product selectivity can reach 90% with
On, there is preferably performance in terms of service life, but the active component species of the catalyst is more, and carrier is also needed to by fluorination
Reason, and because carrier is activated carbon, the process of catalyst regeneration carbon remover can cause carrier depletion, the catalysis after influence regeneration
Agent activity, is unfavorable for improving the overall service life of catalyst.
Above-mentioned each patented technology is still present poor catalyst activity, short life, production during trifluoro-ethylene is produced
The problem of high cost, constrains the large-scale production of trifluoro-ethylene, therefore need to develop a kind of high activity, high stability, low production
The catalyst of cost meets the requirement of trifluoro-ethylene industrialization production.
The content of the invention
The technical problem to be solved in the present invention is to overcome the shortcomings of that existing catalyst is present in background technology, especially for urging
Agent totality service life is short, is difficult the problem of regeneration, there is provided a kind of preparation process is simple, and reactivity worth is efficient, regenerative process
Easy to control, overall long service life can be used for the catalyst of large-scale production trifluoro-ethylene.
A kind of catalyst, with porous metals fluoride or oxyfluoride as carrier, with precious metal palladium or platinum as active component,
It is a kind of as co-catalyst in addition B, Bi, Ni, Co, Ti, V, Mo, W, Cu element, using infusion process preparation, refilter, do
Obtained through activation after dry, roasting；The noble-metal-supported amount be 0.1~50%, the co-catalyst load capacity be 0.01~
10%, the carrier uses preceding use 3-10% salpeter solutions boiling reflux 2-12h, and pH=7 is washed with distilled water to after filtering, does
It is dry standby.
The noble-metal-supported amount is 0.1~10%, and the co-catalyst load capacity is 0.01~5%, carrier specific surface
Product 20-300m2/g。
The metal fluoride is aluminum fluoride, magnesium fluoride, calcirm-fluoride, charomic fluoride, and the oxyfluoride is fluorine alumina, fluorine
Calcium oxide, fluorine magnesia, fluorine chromium oxide, the co-catalyst are the one kind in Bi, Ni, V, Cu element.
The carrier is metal fluoride, and the active component is palladium, and the co-catalyst is Bi, the catalyst mode
It is powder, particle or extrusion bar shaped.
The activation is to be passed through H2/N2Gaseous mixture, to catalyst treatment 12-24h at 100-300 DEG C.
The preparation method of above-mentioned catalyst, comprises the following steps：
1) pretreatment of carrier
Porous metals fluoride used or oxyfluoride carrier need to first use 3-10% salpeter solution boiling reflux 2-12h, mistake
PH=7 is washed with distilled water to after filter, is dried；
2) preparation catalyst
A certain amount of precious metal soluble salt is weighed, with maceration extract A is prepared after dissolving with hydrochloric acid, while weighing a certain amount of helping
Catalyst precursor prepares deionized water dipping liquid B, after maceration extract A and maceration extract B is mixed, adds the load by pretreatment
Body, stands dipping 12-24h, and the catalyst filtration that will have been impregnated is dried；
3) activation of catalyst
Dried catalyst is moved into tube furnace, is passed through H2/N2Gaseous mixture, to activation of catalyst at 100-300 DEG C
12-24h, gained catalyst can be used for catalytic reaction.
The precious metal soluble salt is palladium tetrachloride or chloroplatinic acid, and the co-catalyst presoma is promoter metal
Nitrate, the step 1) in dry to dry 12h, the step 2 at 80 DEG C) in dry to dry 24h at 80 DEG C.
Application of the above-mentioned catalyst in fluorine chlorinated hydrocabon hydrogenation-dechlorination prepares fluorinated hydrocarbons.
The fluorine chlorinated hydrocabon is CTFE, and the fluorinated hydrocarbons is trifluoro-ethylene.
The hydrogenation-dechlorination reaction is vapor phase method, and using fixed bed reactors, hydrogen is passed through simultaneously with CTFE, hydrogen
Gas is 0.5-2 with CTFE mol ratio, and 50-200 DEG C of reaction temperature, total air speed is controlled in 100-1500h-1。
It is preferred that：Hydrogen is 0.5-1.2 with CTFE mol ratio, and 80-150 DEG C of reaction temperature, total air speed control exists
300-800h-1。
The present invention preferred main active component and cocatalyst component, while porous fluoride or oxyfluoride are carried
Body, while using H2/N2Gaseous mixture is used as activated gas so that catalyst of the invention hydrogenation-dechlorination reaction in effect with
Prior art quite, but because carrier is porous fluoride or oxyfluoride, only needs to be flowed back using nitric acid, no in pretreatment
Need to add fluoride to reprocess, while carrier of the invention can hold receipts catalytic reaction temperature higher, in catalyst regeneration except product
The process of carbon can cannot be easily caused carrier depletion, not interfere with the catalyst activity after regeneration, be conducive to improving the total of catalyst
Body service life.
When catalyst of the present invention is used to prepare trifluoro-ethylene, using fixed bed reactors, material is 316 stainless steels,
Internal diameter 20mm, length 600mm, loaded catalyst is 100ml.When carrying out catalytic reaction, reaction temperature is 50-200 DEG C, preferably
80-150 DEG C, hydrogen is 0.5-2, preferably 0.5-1.2 with CTFE mol ratio, and total air speed control is in 100-1500h-1, it is excellent
Select 300-800h-1.Product carries out quantitative analysis after washing, alkali cleaning, drying with GC, calculates feed stock conversion and trifluoro second
Alkene selectivity.
Beneficial effect：
1. catalyst of the present invention has that reactivity is high, target product selectivity in the reaction for prepare trifluoro-ethylene
The characteristics of height, catalyst long service life；
2. the porous metals fluoride or oxyfluoride used by catalyst of the present invention have chemical inertness, will not be reacted
HF, HCl corrosion produced in journey, still have preferably activity after long-lasting catalytic use；
3. the porous metals fluoride or oxyfluoride used by catalyst of the present invention not with oxygen reaction, catalyst regeneration
During will not because of carbon remover and caused by carrier consumption, regenerated catalyst excellent performance can significantly extend catalyst
Service life.
Specific embodiment
With reference to embodiment, the present invention will be further described, but does not limit the invention to these specific embodiment parties
Formula.
Embodiment 1 (sample 1)
Weigh 200g bar shaped aluminum fluorides, add 10% salpeter solution boiling reflux 6h, be washed with deionized after filtering to
PH=7, dries 12h at 80 DEG C, stand-by；
Weigh 1.68g PdCl2Dissolved with concentrated hydrochloric acid, add deionized water 100g to stir to solution clarification, obtain maceration extract
A.Weigh 1.17g Bi (NO3) ﹒ 5H2O 100g deionized water dissolvings, stirring obtains maceration extract B to solution clarification.By maceration extract
A mixes with maceration extract B, adds and stands dipping 12h by the bar shaped aluminum fluoride of pretreatment.After the catalyst filtration that will have been impregnated,
It is stand-by in 24h is dried at 80 DEG C.
Embodiment 2 (sample 2)
Weigh 200g bar shaped magnesium fluorides, add 10% salpeter solution boiling reflux 12h, be washed with deionized after filtering to
PH=7, dries 12h at 80 DEG C, stand-by；
Weigh 3.38g PdCl2Dissolved with concentrated hydrochloric acid, add deionized water 100g to stir to solution clarification, obtain maceration extract
A.Weigh 5.03g Ni (NO3) ﹒ 6H2O 100g deionized water dissolvings, stirring obtains maceration extract B to solution clarification.By maceration extract
A mixes with maceration extract B, adds and stands dipping 12h by the bar shaped magnesium fluoride of pretreatment.After the catalyst filtration that will have been impregnated,
It is stand-by in 24h is dried at 80 DEG C.
Embodiment 3 (sample 3)
Weigh 200g bar shaped calcirm-fluoride, add 5% salpeter solution boiling reflux 18h, be washed with deionized after filtering to
PH=7, dries 24h at 80 DEG C, stand-by；
Weigh 10.36g PdCl2Dissolved with concentrated hydrochloric acid, add deionized water 100g to stir to solution clarification, impregnated
Liquid A.Weigh 3.21g VCl3100g deionized water dissolvings are used, stirring obtains maceration extract B to solution clarification.By maceration extract A and leaching
Stain liquid B mixes, and adds and stands dipping 24h by the bar shaped calcirm-fluoride of pretreatment.After the catalyst filtration that will have been impregnated, in 80 DEG C
Under dry 24h, it is stand-by.
Embodiment 4 (sample 4)
Weigh 200g bar shaped charomic fluorides, add 10% salpeter solution boiling reflux 12h, be washed with deionized after filtering to
PH=7, dries 12h at 80 DEG C, stand-by；
Weigh 6.87g PdCl2Dissolved with concentrated hydrochloric acid, add deionized water 100g to stir to solution clarification, obtain maceration extract
A.Weigh 6.04g Cu (NO3)2100g deionized water dissolvings are used, stirring obtains maceration extract B to solution clarification.By maceration extract A with
Maceration extract B mixes, and adds and stands dipping 12h by the bar shaped charomic fluoride of pretreatment.After the catalyst filtration that will have been impregnated, in 80
24h is dried at DEG C, it is stand-by.
Embodiment 5
The catalyst sample (1-4) of above-mentioned preparation is filled in reactor, loadings 100ml is heated to 150 DEG C, led to
Enter N2/H2Gaseous mixture is to activation of catalyst 24h.120 DEG C are cooled to, adjustment hydrogen is 1.1/ with CTFE raw materials components mole ratio
1, air speed is adjusted to 400h-1, product by being analyzed with GC after washing, alkali cleaning, drying and calculate feed stock conversion and
Trifluoro-ethylene selectivity, experimental result is as shown in table 1：
The sample 1-4 reactivity worth of table 1 is contrasted
Be can see from the contrast of the experimental result of table 1, with palladium as main active component, with porous metals fluoride as carrier,
Prepared catalyst has preferably performance in CTFE prepares trifluoro-ethylene reaction, except the reaction of sample 3 is converted
Beyond rate is less than 90%, other three sample conversion ratios are above 90%, and the wherein catalyst of sample 1 has optimal reactivity worth
Performance.
Embodiment 6 (sample 5)
200g column fluorine aluminas are weighed, 10% salpeter solution boiling reflux 12h is added, is washed with deionized after filtering
To pH=7,12h is dried at 80 DEG C, it is stand-by；
The chloroplatinic acid deionized water dissolvings of 11.24g 38% are weighed, adds deionized water 100g to stir to solution clarification, obtained
To maceration extract A.Weigh 2.37g Bi (NO3)2﹒ 5H2O 100g deionized water dissolvings, stirring obtains maceration extract to solution clarification
B.Maceration extract A is mixed with maceration extract B, is added and is stood dipping 12h by the bar shaped fluorine alumina of pretreatment.By urging for having impregnated
It is stand-by in 24h is dried at 80 DEG C after agent filtering.
Embodiment 7 (sample 6)
200g column fluorine magnesia is weighed, 5% salpeter solution boiling reflux 24h is added, is washed with deionized after filtering
To pH=7,12h is dried at 80 DEG C, it is stand-by；
The chloroplatinic acid deionized water dissolvings of 11.24g 38% are weighed, adds deionized water 100g to stir to solution clarification, obtained
To maceration extract A.Weigh 5.03g Ni (NO3)2﹒ 6H2O 100g deionized water dissolvings, stirring obtains maceration extract to solution clarification
B.Maceration extract A is mixed with maceration extract B, is added and is stood dipping 12h by the bar shaped fluorine magnesia of pretreatment.By urging for having impregnated
It is stand-by in 24h is dried at 80 DEG C after agent filtering.
Embodiment 8 (sample 7)
200g column fluorine calcium oxide is weighed, 5% salpeter solution boiling reflux 24h is added, is washed with deionized after filtering
To pH=7,12h is dried at 80 DEG C, it is stand-by；
The chloroplatinic acid deionized water dissolvings of 5.58g 38% are weighed, adds deionized water 100g to stir to solution clarification, obtained
To maceration extract A.Weigh 1.54g VCl3100g deionized water dissolvings are used, stirring obtains maceration extract B to solution clarification.Will dipping
Liquid A mixes with maceration extract B, adds and stands dipping 24h by the bar shaped fluorine calcium oxide of pretreatment.The catalyst filtration that will have been impregnated
Afterwards, it is stand-by in 24h is dried at 80 DEG C.
Embodiment 9 (sample 8)
200g column fluorine chromium oxide is weighed, 5% salpeter solution boiling reflux 24h is added, is washed with deionized after filtering
To pH=7,12h is dried at 80 DEG C, it is stand-by；
The chloroplatinic acid deionized water dissolvings of 22.78g 38% are weighed, adds deionized water 100g to stir to solution clarification, obtained
To maceration extract A.Weigh 6.04g Cu (NO3)2100g deionized water dissolvings are used, stirring obtains maceration extract B to solution clarification.Will leaching
Stain liquid A mixes with maceration extract B, adds and stands dipping 24h by the bar shaped fluorine chromium oxide of pretreatment.The catalyst mistake that will have been impregnated
It is stand-by in 24h is dried at 80 DEG C after filter.
Embodiment 10
The catalyst sample (5-8) of above-mentioned preparation is filled in reactor, loadings 100ml is heated to 150 DEG C, led to
Enter N2/H2Gaseous mixture is to activation of catalyst 24h.120 DEG C are cooled to, adjustment hydrogen is 1.5/ with CTFE raw materials components mole ratio
1, air speed is adjusted to 300h-1, product by being analyzed with GC after washing, alkali cleaning, drying and calculate feed stock conversion and
Trifluoro-ethylene selectivity, experimental result is as shown in table 2：
The sample 1-4 reactivity worth of table 2 is contrasted
| Catalyst | CTFE conversion ratio, % | Trifluoro-ethylene selectivity, % |
| Sample 5 | 92.1 | 90.2 |
| Sample 6 | 84.7 | 82.3 |
| Sample 7 | 83.5 | 88.7 |
| Sample 8 | 89.6 | 86.1 |
Be can see from the contrast of the experimental result of table 2, be to carry with porous metals oxyfluoride with platinum as main active component
Body, the prepared catalyst catalytic effect in CTFE prepares trifluoro-ethylene reaction is suitable with prior art, sample 5
Reaction conversion ratio is higher than 90%, and other three sample conversion ratios are below 90%.Integrated comparative, the catalyst of sample 1 has optimal
Reactivity worth.
Embodiment 11
According to the evaluation method in embodiment 5, stability test is carried out to sample 1, the data obtained is shown in Table 3.Therefrom can be with
See, after catalyst operation 1500h, CTFE conversion ratio only declines 2.2%, and trifluoro-ethylene selectivity is left 96% always
The right side, catalyst not only maintains reactivity very high, while also having good stability.
The catalyst life evaluation experimental result of table 3
| Reaction time, h | CTFE conversion ratio, % | Trifluoro-ethylene selectivity, % |
| 100 | 94.1% | 96.3% |
| 200 | 94.6% | 96.2% |
| 400 | 93.4% | 97.2% |
| 800 | 92.7% | 96.0% |
| 1000 | 92.6% | 95.4% |
| 1200 | 92.3% | 95.9% |
| 1500 | 91.9% | 97.2% |
Embodiment 12
To being regenerated using the catalyst after 1500h：High reaction temperature is risen to 200 DEG C, N is passed through2- air Mixture pair
Catalyst regenerates 24h, wherein N2/ air=5/1, after in tail gas without obvious carbon dioxide after (clarification limewash detection),
It is cooled to 150 DEG C.Catalyst is reactivated according to activation of catalyst program, according to appreciation condition in embodiment 5 after the completion of activation
Regenerated catalyst activity is evaluated, as shown in table 4：
The regenerated catalyst reaction effect of table 4 is evaluated
| Reaction time, h | CTFE conversion ratio, % | Trifluoro-ethylene selectivity, % |
| 100 | 93.1% | 96.4% |
| 200 | 92.3% | 95.8% |
| 400 | 91.8% | 95.6% |
| 800 | 90.3% | 96.1% |
As can be seen from Table 4, the catalyst after regeneration still maintains preferable reaction effect, and feed stock conversion is higher than
90%, trifluoro-ethylene selectivity about 96%.
Claims (10)
1. a kind of catalyst, with porous metals fluoride or oxyfluoride as carrier, with precious metal palladium or platinum as active component, adds
Plus it is a kind of as co-catalyst in B, Bi, Ni, Co, Ti, V, Mo, W, Cu element, using infusion process preparation, refilter, dry,
Obtained through activation after roasting；The noble-metal-supported amount be 0.1~50%, the co-catalyst load capacity be 0.01~
10%, the carrier uses preceding use 3-10% salpeter solutions boiling reflux 2-12h, and pH=7 is washed with distilled water to after filtering, does
It is dry standby.
2. catalyst according to claim 1, the noble-metal-supported amount is 0.1~10%, the co-catalyst load
It is 0.01~5% to measure, carrier specific surface area 20-300m2/g。
3. catalyst according to claim 1, the metal fluoride is aluminum fluoride, magnesium fluoride, calcirm-fluoride, charomic fluoride,
The oxyfluoride is fluorine alumina, fluorine calcium oxide, fluorine magnesia, fluorine chromium oxide, and the co-catalyst is Bi, Ni, V, Cu unit
One kind in element.
4. catalyst according to claim 3, the carrier is metal fluoride, and the active component is palladium, described to help
Catalyst is Bi, and the catalyst mode is powder, particle or extrusion bar shaped.
5., according to the preparation method of any catalyst of claim 1-4, comprise the following steps：
1) pretreatment of carrier
Porous metals fluoride used or oxyfluoride carrier need to first use 3-10% salpeter solution boiling reflux 2-12h, after filtering
PH=7 is washed with distilled water to, is dried；
2) preparation catalyst
A certain amount of precious metal soluble salt is weighed, with maceration extract A is prepared after dissolving with hydrochloric acid, while weighing a certain amount of co-catalysis
Agent presoma prepares deionized water dipping liquid B, after maceration extract A and maceration extract B is mixed, adds the carrier by pretreatment, quiet
Dipping 12-24h is put, the catalyst filtration that will have been impregnated is dried；
3) activation of catalyst
Dried catalyst is moved into tube furnace, is passed through H2/N2Gaseous mixture, to activation of catalyst 12- at 100-300 DEG C
24h, gained catalyst can be used for catalytic reaction.
6. preparation method according to claim 5, the precious metal soluble salt is palladium tetrachloride or chloroplatinic acid, described to help
Catalyst precursor is the nitrate of promoter metal, the step 1) in dry to dry 12h, the step 2 at 80 DEG C)
Middle drying be 80 DEG C at dry 24h.
7. the application according to any catalyst of claim 1-4 in fluorine chlorinated hydrocabon hydrogenation-dechlorination prepares fluorinated hydrocarbons.
8. application according to claim 7, the fluorine chlorinated hydrocabon is CTFE, and the fluorinated hydrocarbons is trifluoro-ethylene.
9. application according to claim 8, the hydrogenation-dechlorination reaction is vapor phase method, using fixed bed reactors, hydrogen
It is passed through simultaneously with CTFE, hydrogen is 0.5-2,50-200 DEG C of reaction temperature, total air speed control with CTFE mol ratio
System is in 100-1500h-1。
10. application according to claim 5, the hydrogen is 0.5-1.2, reaction temperature with CTFE mol ratio
80-150 DEG C, total air speed control is in 300-800h-1。
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| CN109967101A (en) * | 2019-05-08 | 2019-07-05 | 西安近代化学研究所 | A kind of selection hydrogenation-dechlorination preparation chlorotrifluoroethylene catalyst |
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